US4913801A - Passivation of FCC catalysts - Google Patents
Passivation of FCC catalysts Download PDFInfo
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- US4913801A US4913801A US07/208,202 US20820288A US4913801A US 4913801 A US4913801 A US 4913801A US 20820288 A US20820288 A US 20820288A US 4913801 A US4913801 A US 4913801A
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- cerium
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
- C10G2300/705—Passivation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S502/00—Catalyst, solid sorbent, or support therefor: product or process of making
- Y10S502/521—Metal contaminant passivation
Definitions
- This invention relates to the art of catalytic cracking of hydrocarbons, and in particular to methods of inhibiting on zeolite catalysts the detrimental effects of contamination by metals, particularly nickel, which are contained in the hydrocarbon feedstock.
- FCC Fluid Catalytic Cracker
- Major metal contaminants that are found in Fluid Catalytic Cracker (FCC) feedstocks include nickel, vanadium, iron, copper and occasionally other heavy metals.
- the problems associated with metal contamination, particularly nickel, during the catalytic cracking of hydrocarbons to yield light distillates such as gasoline are documented in Oil & Gas Journal of July 6, 1981 on pages 103-111 and of Oct. 31, 1983 on pages 128-134.
- the problems associated with vanadium metal contamination are described in U.S. Pat. No. 4,432,890 and German Pat. No. 3,634,304.
- the invention herein represents an innovation and improvement over those processes set forth and claimed in U.S. Pat. No. 4,432,890 and German Pat. No. 3,634,304.
- Vanadium primarily decreases activity and desirable gasoline selectivity by attacking and destroying the zeolite catalytic sites. Its effect on the activity is about four times greater than that of nickel. Vanadium also increases hydrogen and coke, but at only about one fourth the rate of nickel.
- the reducing atmosphere of hydrogen and carbon monoxide in the cracking zone reduces the nickel and vanadium to lower valence states.
- the nickel is an active dehydrogenating agent under these circumstances, increasing hydrogen and coke which also leads to a small decrease in conversion activity.
- conversion can be increased by changing the catalyst to oil ratio or by increasing the cracking temperature, but coke and hydrogen will also be increased in either case.
- the activity should be kept at a constant level.
- the passivating agents have been added to the catalyst during manufacture, to the catalyst after manufacture by impregnation, to the feedstock before or during processing, to the regenerator, and/or any combination of the above methods.
- cerium passivates vanadium, it was quite unexpectedly found that cerium also passivates the adverse effects of nickel.
- U.S. Pat. Nos. 4,432,890 and 4,513,093 teach that numerous metallic compounds (titanium, zirconium, manganese, magnesium, calcium, strontium, barium, scandium, yttrium, lanthanides, rare earths, actinides, hafnium, tantalum, nickel, indium, bismuth, and tellurium act as vanadium passivators.
- German Pat. No. 3,634,304 claims that yttrium, lanthanides, cerium, and other rare earth compounds passivate the adverse effects of vanadium.
- only titanium was used on an FCC catalyst to show the effects of the various claimed metals on passivating vanadium. Cerium was not specifically mentioned.
- the invention is directed to a process of passivating nickel containing on a zeolitic cracking catalyst.
- the total process generally entails:
- the catalyst during the cracking process in contaminated with from about 100 to 5000 parts nickel per million parts of catalyst, with nickel contained in a feedstock at concentrations of up to about 100 ppm, which nickel would increase hydrogen and coke yields at the cracking temperatures and conditions in the cracking zone, and wherein the catalyst contains less than about 3000 ppm of vanadium; the improvement comprising treating the feedstock containing the nickel contaminant with cerium, with the amount of cerium utilized being from 0.005 to 240 ppm on the nickel in the feedstock and at atomic ratios with nickel of from 1:1 to 0.05:1 Ce/Ni, preferable 0.66:1to 0.1:1.
- cerium compounds which can be used include cerium in the cerous or ceric state with anions of nitrate (designated NO 3 in the examples), ammonium nitrate, acetate, proprionate, butyrate, neopentoate, octoate (Oct), laurate, neodecanoate, stearate, naphthenate, oxalate, maleate, benzoate, acrylate, salicylate, versalate, terephthalate, carbonate, hydroxide, sulfate, fluoride, organosulfonate, acetylacetonate, Beta-diketones, oxide (designated either as O 2 for a water based suspension or as Org for a hydrocarbon based suspension in the examples), ortho-phosphate, or combinations of the above.
- the cerium compound is fed to the feedstock on a continuous basis so that enough cerium is present in the feedstock to passivate the nickel contained therein.
- the cerium concentration in the feedstock will be 0.005 to 240 ppm based on 0.1 to 100 ppm nickel in the feedstock.
- the most desirable manner of treating the cracking catalyst with the cerium will be adding a solution or suspension containing the cerium to the feedstock.
- the solvent used to solubilize or suspend the cerium compound can be water or an organic solvent, preferably a hydrocarbon solvent similar to the hydrocarbon feedstock.
- the concentration of the cerium in the solvent can be any concentration that makes it convenient to add the cerium to the feedstock.
- zeolite crystalline aluminosilicate cracking catalysts were used.
- the catalytic cracking runs were conducted employing a fixed catalyst bed, a temperature of 482° C., a contact time of 75 seconds, and a catalyst to oil ratio of about 3:1 or greater as detailed under the catalyst to oil ratio (C/O) in the individual Tables.
- the feedstock used for these cracking runs was a gas oil feedstock having a boiling range of approximately 500° to 1000° F.
- the four zeolitic cracking catalysts that were used are all commercial catalysts that are described as:
- Each of the four catalysts were conditioned similarly.
- the fresh Catalysts A, C, and D were heated in air to 649° C. for 0.5 hour before metals were added.
- To these conditioned catalysts were added the appropriate ppms of vanadium, and/or nickel, and/or cerium (as designated in the Tables) followed by heating the metals contaminated catalysts in air for 1 hour at 649° C. and then for 6.5 hours in steam at 732° C., or 760° C., or 788° C.
- Catalyst B was heated in air at 649° C. for 0.5 hour before metals were added.
- To the conditioned catalyst was added the appropriate ppms of vanadium and/or nickel and/or cerium (as designated in Table 2) followed by heating the metals contaminated catalyst in air for 1 hour at 649° C. and then for 19.5 hours at 732° C. in steam.
- Predicted hydrogen weight percent data were determined by a least squares linear fit of the vanadium and/or nickel contaminated catalyst runs for each catalyst. Predicted catalyst hydrogen weight percent data were determined by a least squares fit of the fresh catalysts only. The equations determined in each case are given in the appropriate tables.
- Catalyst D the percent changes in hydrogen and coke were reduced when passivated with cerium compounds.
Abstract
The present invention is directed to a method of using cerium and/or cerium contaning compounds to passivate nickel contaminants in hydrocarbon feedstocks which are used in catalytic cracking processes.
Description
This invention relates to the art of catalytic cracking of hydrocarbons, and in particular to methods of inhibiting on zeolite catalysts the detrimental effects of contamination by metals, particularly nickel, which are contained in the hydrocarbon feedstock.
Major metal contaminants that are found in Fluid Catalytic Cracker (FCC) feedstocks include nickel, vanadium, iron, copper and occasionally other heavy metals. The problems associated with metal contamination, particularly nickel, during the catalytic cracking of hydrocarbons to yield light distillates such as gasoline are documented in Oil & Gas Journal of July 6, 1981 on pages 103-111 and of Oct. 31, 1983 on pages 128-134. The problems associated with vanadium metal contamination are described in U.S. Pat. No. 4,432,890 and German Pat. No. 3,634,304. The invention herein represents an innovation and improvement over those processes set forth and claimed in U.S. Pat. No. 4,432,890 and German Pat. No. 3,634,304.
It is well known in the art that nickel significantly increases hydrogen and coke and can cause decreases in catalyst activity. Vanadium primarily decreases activity and desirable gasoline selectivity by attacking and destroying the zeolite catalytic sites. Its effect on the activity is about four times greater than that of nickel. Vanadium also increases hydrogen and coke, but at only about one fourth the rate of nickel.
The reducing atmosphere of hydrogen and carbon monoxide in the cracking zone reduces the nickel and vanadium to lower valence states. The nickel is an active dehydrogenating agent under these circumstances, increasing hydrogen and coke which also leads to a small decrease in conversion activity.
Vanadium has been shown to destroy active catalytic sites by the movement of the volatile vanadium pentoxide through the catalyst structure. Lower oxides of vanadium are not volatile and are not implicated in the destruction of catalyst activity. In the cracking zone, lower oxides of vanadium will be present and vanadium pentoxide will be absent. Thus in the cracking zone, fresh vanadium from the feedstock will not reduce activity. When the lower valence vanadium compounds enter the regenerator where oxygen is present to combust the coke, the vanadium compounds are oxidized to vanadium pentoxide which then can migrate to active sites and destroy the active sites, leading to a large reduction in activity and selectivity, particularly gasoline.
An increase in hydrogen and coke due to contaminant metals translates to a decrease in yields of desirable products such as gasoline and light gases (propane/butanes). Also, increases in hydrogen yield require extensive processing to separate the cracked products and can result in operation and/or compressor limitations.
While the coke that is produced during the catalytic cracking process is used to keep the unit in heat balance, increases in coke yields mean increased temperatures in the regenerator which can damage catalysts by destroying the zeolitic structures and thus decrease activity.
As activity is destroyed by contaminant metals, conversion can be increased by changing the catalyst to oil ratio or by increasing the cracking temperature, but coke and hydrogen will also be increased in either case. For best efficiency in a FCC unit, the activity should be kept at a constant level.
However, as vandium is deposited on the catalyst over and above about a 3,000 ppm level, significant decreases in activity occur. Passivators have been used to offset the detrimental effects of nickel and of vanadium.
Numerous passivating agents have been taught and claimed in various patents for nickel. Some examples include antimony in U.S. Pat. Nos. 3,711,422, 4,025,458, 4,111,845, and sundry others; bismuth in U.S. Pat. Nos. 3,977,963 and 4,141,858; tin in combination with antimony in U.S. Pat. No. 4,255,287; germanium in U.S. Pat. No. 4,334,979; gallium in U.S. Pat. No. 4,377,504, tellurium in U.S. Pat. No. 4,169,042; indium in U.S. Pat. No. 4,208,302; thallium in U.S. Pat. No. 4,238,367; manganese in U.S. Pat. No. 3,977,963; aluminum in U.S. Pat. No. 4,289,608; zinc in U.S. Pat. No. 4,363,720; lithium in U.S. Pat. No. 4,364,847; barium in U.S. Pat. No. 4,377,494; phosphorus in U.S. Pat. No. 4,430,199; titanium and zirconium in U.S. Pat. No. 4,437,981; silicon in U.S. Pat. No. 4,319,983; tungsten in U.S. Pat. No. 4,290,919; and boron in U.S. Pat. No. 4,295,955.
Examples of vanadium passivating agents are fewer, but include tin in U.S. Pat. No. 4,101,417 and 4,601,815; titanium, zirconium, manganese, magnesium, calcium, strontium, barium, scandium, yttrium, lanthanides, rare earths, actinides, hafnium, tantalum, nickel, indium, bismuth, and tellurium in U.S. Pat. Nos. 4,432,890 and 4,513,093; yttrium, lanthanum, cerium and the other rare earths in German 3,634,304.
In general, the passivating agents have been added to the catalyst during manufacture, to the catalyst after manufacture by impregnation, to the feedstock before or during processing, to the regenerator, and/or any combination of the above methods.
It was discovered that when a zeolite catalyst contaiminated with metals, including nickel, is treated with cerium compounds, the hydrogen-forming property of the nickel was mitigated to a great extent.
While cerium passivates vanadium, it was quite unexpectedly found that cerium also passivates the adverse effects of nickel.
U.S. Pat. Nos. 4,432,890 and 4,513,093 teach that numerous metallic compounds (titanium, zirconium, manganese, magnesium, calcium, strontium, barium, scandium, yttrium, lanthanides, rare earths, actinides, hafnium, tantalum, nickel, indium, bismuth, and tellurium act as vanadium passivators. German Pat. No. 3,634,304 claims that yttrium, lanthanides, cerium, and other rare earth compounds passivate the adverse effects of vanadium. In the '890 patent, only titanium was used on an FCC catalyst to show the effects of the various claimed metals on passivating vanadium. Cerium was not specifically mentioned. In each of these patents, nickel was not added to the catalyst undergoing testing and so the effects on hydrogen-make by nickel with cerium passivation could not be observed. In addition, the only vanadium levels tested in these two patents were 5,500 and 3,800 ppm, respectively. Although nickel and vanadium contamination of FCC catalysts is discussed in great depth in the art and in the same context, it is equally clear from the specifics of the art, that each represents its own separate problem as well as solution. It is not evident or expected that any treatment for vanadium would also be effective for nickel or vice-versa.
It is well documented in the art that a certain level of vanadium is necessary on the catalyst to observe a loss of catalyst activity. This level varies with the type of catalyst. In one report the level of vanadium below which catalyst activity is not degraded is 1,000 ppm for that catalyst (see the newsletter Catalagram published by Davison Chemical in 1982, Issue Number 64). In another article (R. F. Wormsbecher, et al., J. Catal., 100, 130-137(1986)), only above 2000 ppm vanadium are catalyst activity and selectivity lost. Other catalysts such as metal resistant catalysts need high levels (above about 3000 ppm) of vanadium where loss of catalyst activity can be observed (Oil & Gas Journal, 103-111, July 6, 1981). From these articles, it can be seen that not all catalysts are significantly affected by lower levels of vanadium contaminant.
Thus, the treatment of specific catalysts containing less than a significant level of vanadium would show very small to insignificant changes in activity on addition of cerium. However, the practical effects of nickel can be observed at levels as low as about 300 ppm, with the amount of hydrogen and coke increasing proportional to the amount of nickel present.
As earlier indicated, the invention is directed to a process of passivating nickel containing on a zeolitic cracking catalyst.
The total process generally entails:
a. Contacting a hydrocarbon feedstock with a fluidized zeolite-containing cracking catalyst in a cracking zone under cracking conditions;
b. recovering the cracked products;
c. passing the cracking catalyst from the cracking zone to a regeneration zone;
d. regenerating the cracking catalyst in the regeneration zone by contact with oxygen-containing gas under regeneration conditions to produce a regenerated catalyst; and
e. introducing the regenerated catalyst to the cracking zone for contact with the hydrocarbon feedstock;
wherein the catalyst during the cracking process in contaminated with from about 100 to 5000 parts nickel per million parts of catalyst, with nickel contained in a feedstock at concentrations of up to about 100 ppm, which nickel would increase hydrogen and coke yields at the cracking temperatures and conditions in the cracking zone, and wherein the catalyst contains less than about 3000 ppm of vanadium; the improvement comprising treating the feedstock containing the nickel contaminant with cerium, with the amount of cerium utilized being from 0.005 to 240 ppm on the nickel in the feedstock and at atomic ratios with nickel of from 1:1 to 0.05:1 Ce/Ni, preferable 0.66:1to 0.1:1.
Although it is not important as to the form in which the cerium is added to the feedstock, examples of cerium compounds which can be used include cerium in the cerous or ceric state with anions of nitrate (designated NO3 in the examples), ammonium nitrate, acetate, proprionate, butyrate, neopentoate, octoate (Oct), laurate, neodecanoate, stearate, naphthenate, oxalate, maleate, benzoate, acrylate, salicylate, versalate, terephthalate, carbonate, hydroxide, sulfate, fluoride, organosulfonate, acetylacetonate, Beta-diketones, oxide (designated either as O2 for a water based suspension or as Org for a hydrocarbon based suspension in the examples), ortho-phosphate, or combinations of the above.
Generally the cerium compound is fed to the feedstock on a continuous basis so that enough cerium is present in the feedstock to passivate the nickel contained therein. The cerium concentration in the feedstock will be 0.005 to 240 ppm based on 0.1 to 100 ppm nickel in the feedstock.
The most desirable manner of treating the cracking catalyst with the cerium will be adding a solution or suspension containing the cerium to the feedstock. The solvent used to solubilize or suspend the cerium compound can be water or an organic solvent, preferably a hydrocarbon solvent similar to the hydrocarbon feedstock. The concentration of the cerium in the solvent can be any concentration that makes it convenient to add the cerium to the feedstock.
More detailed information relative to the invention will be evident from the following specific embodiments.
In the Examples shown, commercially available zeolite crystalline aluminosilicate cracking catalysts were used. The catalytic cracking runs were conducted employing a fixed catalyst bed, a temperature of 482° C., a contact time of 75 seconds, and a catalyst to oil ratio of about 3:1 or greater as detailed under the catalyst to oil ratio (C/O) in the individual Tables. The feedstock used for these cracking runs was a gas oil feedstock having a boiling range of approximately 500° to 1000° F.
The four zeolitic cracking catalysts that were used are all commercial catalysts that are described as:
Catalyst A--yielding maximum octane enhancement and lowest coke and gas,
Catalyst B--yielding highest liquid product selectivity and low gas and coke make,
Catalyst C--yielding highest activity for octane enhancement and stability with low coke and gas make, and
Catalyst D--yielding octane enhancement and high stability with low coke and gas make.
Each of the four catalysts were conditioned similarly. The fresh Catalysts A, C, and D were heated in air to 649° C. for 0.5 hour before metals were added. To these conditioned catalysts were added the appropriate ppms of vanadium, and/or nickel, and/or cerium (as designated in the Tables) followed by heating the metals contaminated catalysts in air for 1 hour at 649° C. and then for 6.5 hours in steam at 732° C., or 760° C., or 788° C.
Catalyst B was heated in air at 649° C. for 0.5 hour before metals were added. To the conditioned catalyst was added the appropriate ppms of vanadium and/or nickel and/or cerium (as designated in Table 2) followed by heating the metals contaminated catalyst in air for 1 hour at 649° C. and then for 19.5 hours at 732° C. in steam.
The procedure utilized to test the efficacy of the zeolite catalysts treated in accordance with the present invention is that which is outlined in the ASTM-D-3907, which is incorporated herein by reference.
The weight percent changes in conversion were calculated in the following manner:
Weight % Change Conversion=Wt. % conv. Ce run--Avg. Wt. % conv. metals contaminant runs
The percent changes in hydrogen make were calculated in the following manner: ##EQU1##
Predicted hydrogen weight percent data were determined by a least squares linear fit of the vanadium and/or nickel contaminated catalyst runs for each catalyst. Predicted catalyst hydrogen weight percent data were determined by a least squares fit of the fresh catalysts only. The equations determined in each case are given in the appropriate tables.
The percent changes in coke were calculated in the following manner: ##EQU2##
TABLE 1
__________________________________________________________________________
Data for FCC Commercial Catalyst A
Avg. Actual Molar Ratios
% Change In
Ce Ce V Ni Nos.
Wt. %
Wt. %
Wt. %
Ce/ Ce/ Wt. %
Cmpd ppm ppm ppm C/O Test
Conv.
H.sub.2
Coke
Ni V + Ni
Conv.
H.sub.2
Coke
__________________________________________________________________________
Steaming Temperature = 732° C.
None 0 0 0 3.00
1 68.9
0.06 1.5 -- -- -- -- --
None 0 3000 1500 3.00
2 55.5
0.59 3.0 0.00
0.00 0 0 0
O.sub.2
3000 3000 1500 3.00
2 54.5
0.60 2.2 0.84
0.25 -1 2 -25
Oct 3000 3000 1500 3.00
2 58.3
0.56 2.6 0.84
0.25 4 -6 -12
None 0 0 3000 3.00
2 65.9
0.63 3.7 0.00
0.00 0 0 0
O.sub.2
1500 0 3000 3.00
2 59.1
0.54 2.2 0.21
0.21 -7 -16 -41
Oct 1500 0 3000 3.00
2 59.7
0.50 2.9 0.21
0.21 -6 -22 -21
Steaming Temperature = 760° C.
None 0 0 0 3.03
2 56.5
0.06 1.1 -- -- -- -- --
None 0 0 0 4.44
2 70.5
0.07 3.3 -- -- -- -- --
None 0 0 2000 3.02
4 53.5
0.42 2.4 0.00
0.00 0 0 0
None 0 0 2000 4.44
4 66.2
0.63 2.8 0.00
0.00 0 0 0
None 0 0 2000 5.95
2 75.6
0.94 3.7 0.00
0.00 0 0 0
Oct 1000 0 2000 2.96
1 62.5
0.36 4.2 0.21
0.21 6 -45 71
Oct 1000 0 2000 4.55
2 79.5
0.63 6.8 0.21
0.21 13 -38 146
Oct 2000 0 2000 3.02
1 63.6
0.35 4.5 0.42
0.42 10 -49 86
Oct 2000 0 2000 4.39
1 68.8
0.51 5.1 0.42
0.42 3 -34 85
Oct 3000 0 2000 4.30
1 70.3
0.43 5.8 0.63
0.63 4 -49 110
Oct 3000 0 2000 2.97
1 57.2
0.32 3.7 0.63
0.63 4 -38 52
Steaming Temperature = 788° C.
None 0 0 0 2.94
2 49.0
0.04 0.04
-- -- -- -- --
None 0 0 0 4.47
2 71.4
0.06 4.1 -- -- -- -- --
None 0 0 2000 2.96
4 42.4
0.33 2.7 0.00
0.00 0 0 0
None 0 0 2000 4.43
4 56.2
0.56 3.1 0.00
0.00 0 0 0
None 0 0 2000 6.01
2 68.5
0.83 2.6 0.00
0.00 0 0 0
Oct 1000 0 2000 4.56
1 55.3
0.47 3.8 0.21
0.21 -1 -19 21
Oct 1000 0 2000 2.93
1 43.8
0.30 2.2 0.21
0.21 1 -14 -20
Oct 2000 0 2000 3.08
1 45.4
0.27 2.3 0.42
0.42 3 -30 -16
Oct 2000 0 2000 4.54
1 50.0
0.42 3.0 0.42
0.42 -6 -13 -4
Oct 3000 0 2000 3.01
1 43.1
0.27 2.2 0.63
0.63 1 -22 -18
Oct 3000 0 2000 4.57
1 58.4
0.41 3.8 0.63
0.63 2 -33 21
__________________________________________________________________________
Predicted Hydrogen Weight %:
at 760° C. = 0.00104*C/O + 0.0226*conv. - 0.823
at 788° C. = 0.0196*C/O + 0.0168*conv. - 0.449
Predicted Cat. H.sub.2 = 0.000778*conv. + 0.0107
It is apparent from the percent change of hydrogen data in Table 1 that cerium in the form of the octoate (Oct) greatly decreases the amount of hydrogen make that is attributed to the nickel contamination. Additionally, the weight percent changes in the conversions are relatively small. Also, the catalysts passivated with cerium resulted in lower coke values when steamed at 732° C. or 788° C.
TABLE 2
__________________________________________________________________________
Data for FCC Commercial Catalyst B
Avg. Actual Molar Ratios
% Change In
Ce Ce V Ni Nos.
Wt. %
Wt. %
Wt. %
Ce/
Ce/
Ce/ Wt. %
Cmpd
ppm ppm ppm Test
Conv.
H.sub.2
Coke
V Ni V + Ni
Conv.
H.sub.2
Coke
__________________________________________________________________________
Steaming Temperature = 732° C.
None
0 0 0 9 74.1
0.08
4.4 0.00
-- -- -- --
None
0 3000 1500 23 62.1
0.46
3.7 0.00
0.00
0.00 0 0 0
NO.sub.3
1500 3000 1500 3 62.8
0.55
2.5 0.18
0.42
0.31 1 32 -31
NO.sub.3
2000 3000 1500 2 61.4
0.49
2.6 0.24
0.56
0.17 -1 16 -19
NO.sub.3
3000 3000 1500 3 64.1
0.38
2.3 0.36
0.84
0.25 2 -16 -38
NO.sub.3
4000 3000 1500 3 66.4
0.52
3.0 0.49
1.12
0.34 4 13 -19
NO.sub. 3
8000 3000 1500 3 64.3
0.54
4.1 0.97
2.25
0.68 2 16 11
O.sub.2
500 3000 1500 5 62.1
0.47
4.0 0.06
0.14
0.04 0 2 10
O.sub.2
1000 3000 1500 4 62.7
0.48
3.7 0.12
0.28
0.08 1 5 2
O.sub.2
1500 3000 1500 2 60.6
0.56
3.3 0.18
0.42
0.13 -2 27 -9
O.sub.2
2000 3000 1500 8 66.1
0.58
3.8 0.24
0.56
0.17 4 26 3
O.sub.2
4000 3000 1500 3 71.6
0.36
3.1 0.49
1.12
0.34 9 -39 -17
O.sub.2
8000 3000 1500 3 67.3
0.45
3.7 0.97
2.25
0.68 5 -11 2
Oct 750 3000 1500 3 65.4
0.48
4.9 0.09
0.21
0.06 3 -8 34
Oct 1500 3000 1500 3 63.3
0.46
4.7 0.18
0.42
0.13 1 -8 29
Oct 3000 3000 1500 2 72.9
0.36
3.8 0.36
0.84
0.25 11 -45 4
Org 1000 3000 1500 3 64.6
0.46
5.3 0.12
0.28
0.08 3 -13 44
Org 2000 3000 1500 3 64.0
0.44
3.5 0.24
0.56
0.17 2 -5 -5
Org 4000 3000 1500 3 62.9
0.48
3.5 0.49
1.12
0.34 1 5 -3
Org 5000 3000 1500 2 68.9
0.47
3.4 0.61
1.40
0.42 7 -8 -7
__________________________________________________________________________
Predicted Weight % H.sub.2 = 0.0070*Conv. - 0.024*Coke - 0.063
From the data in Table 2, it is apparent that cerium reduces hydrogen make especially when the cerium is in the form of an organic compound, and in particular the octoate. At the same time, the increases in conversion are small, except when 3000 to 5000 ppm cerium for various compounds was used. Considering the 3000 ppm of vanadium on the present Catalyst B versus the 3800 ppm of vanadium on the catalyst in German Pat. No. 3,634,304, the change in percent conversion is much smaller in our case (about 12%) versus the case (about 24%) in German Pat. No. 3,634,304. Thus, the cerium is a better passivator of nickel than vanadium. Also, the catalysts passivated with cerium had some effects on coke reduction in these experiments.
TABLE 3
__________________________________________________________________________
Data for FCC Commercial Catalyst C
Avg. Actual Molar
% Change In
Ce Ni Nos.
Wt. %
Wt. %
Wt. %
Ratio
Wt. %
Ce ppm ppm C/O
Test
Conv.
H.sub.2
Coke
Ce/Ni
Conv.
H.sub.2
Coke
__________________________________________________________________________
Steaming Temperature = 760° C.
None
0 0 3.03
2 67.1
0.08
3.0 -- -- -- --
None
0 0 4.55
2 76.3
0.12
4.5 -- -- -- --
None
0 2000 3.02
4 59.5
0.50
2.4 0.00
0 0 0
None
0 2000 4.49
4 70.7
0.70
3.7 0.00
0 0 0
Oct 1500 2000 2.96
1 55.8
0.41
2.9 0.32
-4 -20 21
Oct 1500 2000 4.45
1 73.9
0.63
3.7 0.32
4 -9 0
Oct 3000 2000 2.94
1 59.9
0.52
2.2 0.63
0 7 -11
Oct 3000 2000 4.43
1 72.5
0.64
3.7 0.63
2 -8 0
Oct 1500 0 2.93
1 59.8
0.07
2.2 0.00
-7 9 -26
Oct 1500 0 4.55
1 72.5
0.12
3.8 0.00
-4 30 -16
Steaming Temperature = 788° C.
None
0 0 3.01
2 50.9
0.09
1.9 -- -- -- --
None
0 0 4.55
2 64.5
0.12
2.3 -- -- -- --
None
0 2000 3.06
4 52.8
0.47
2.6 0.00
0 0
None
0 2000 4.50
4 63.3
0.72
3.2 0.00
0 0
Oct 1500 2000 3.00
2 41.7
0.51
2.3 0.32
-11 9 -15
Oct 1500 2000 4.36
1 57.4
0.74
3.7 0.32
-6 6 15
Oct 3000 2000 2.97
1 32.1
0.54
2.3 0.63
-21 15 -15
Oct 3000 2000 4.30
1 56.7
0.61
2.9 0.63
-6 -14 -9
Oct 1500 0 3.08
1 41.3
0.25
1.5 0.00
-10 260 -18
Oct 1500 0 4.49
1 57.5
0.30
2.2 0.00
-7 200 0
__________________________________________________________________________
Predicted Hydrogen Weight %:
at 760° C. = 0.162*C/O - 0.00333*conv. + 0.2085
at 788° C. = 0.176*C/O - 0.000597*conv. - 0.0317
Predicted Cat. H.sub.2 :
at 760° C. = 0.00404*conv. - 0.19
at 788° C. = 0.00196*conv. - 0.00885
For the data in Table 3, only slight improvements can be noted in reducing hydrogen make. It should be noted that when cerium alone was added to the catalyst, large increases in hydrogen make were observed and small decreases in activity were also noted. Thus, overfeeding of cerium could be detrimental to catalyst activity and hydrogen make.
TABLE 4
__________________________________________________________________________
Data for FCC Commercial Catalyst D
Avg. Actual Molar Ratios
% Change In
Ce V Ni Nos.
Wt. %
Wt. %
Wt. %
Ce/
Ce/ Wt. %
Ce ppm ppm ppm Test
Conv.
H.sub.2
Coke
Ni V + Ni
Conv.
H.sub.2
Coke
__________________________________________________________________________
Steaming Temperature = 732° C.
None
0 0 0 4 77.5
0.05
3.6 -- -- -- -- --
None
0 3000 1500 5 64.4
0.56
3.3 0.00
0.00 0 0 0
NO.sub.3
3000 3000 1500 1 68.4
0.53
3.1 0.84
0.25 4 -6 -7
Oct 3000 3000 1500 1 69.7
0.53
3.4 0.84
0.25 5 -6 2
None
0 0 4000 3 75.6
0.62
4.9 0.00
0.00 0 0 0
NO.sub.3
3000 0 4000 1 72.0
0.52
3.0 0.32
0.32 -4 -18 -39
Oct 3000 0 4000 1 74.8
0.70
3.7 0.32
0.32 -1 14 -24
__________________________________________________________________________
For Catalyst D, the percent changes in hydrogen and coke were reduced when passivated with cerium compounds.
For completeness, all data obtained during these experiments have been included. Efforts to exclude any value outside acceptable test error limits have not been made. It is believed that, during the course of these experiments, possible errors in preparing samples and in making measurements may have been made which may account for the occasional data point that is not supportive of this art.
It is apparent from the foregoing that catalysts treated in accordance with the procedures and treatment levels are prescribed by the present innovation permitted reduction in hydrogen attributed primarily to the nickel contaminant.
While this invention has been described with respect to particular embodiments thereof, it is apparent that numerous other forms and modifications of this invention will be obvious to those skilled in the art. The appended claims and this invention generally should be construed to cover all such obvious forms and modifications which are within the true spirit and scope of the present invention.
Claims (8)
1. In a method for cracking a hydrocarbon which comprises:
a. contacting a hydrocarbon feedstock with a fluidized zeolite-containing cracking catalyst in a cracking zone under cracking conditions;
b. recovering the cracked products;
c. passing the cracking catalyst from the cracking zone to a regeneration zone;
d. regenerating the cracking catalyst in the regeneration zone by contact with oxygen-containing gas under regeneration conditions to produce a regenerated catalyst; and
e. introducing the regenerated catalyst to the cracking zone for contact with the hydrocarbon feedstock;
wherein the catalyst during the cracking process is contaminated with from about 100 to 5000 parts nickel per million parts of catalyst, with nickel contained in a feedstock at concentrations of up to about 100 ppm, wherein nickel increases hydrogen and coke yields at the cracking temperatures and conditions in the cracking zone, and wherein the catalyst contains less than about 3000 ppm of vanadium;
the improvement comprising treating the feedstock containing the nickel contamination with cerium, with the amount of cerium utilized being from 0.005 to 240 ppm based on the concentration of the nickel in the feedstock and at atomic ratios with nickel of from 1:1 to 0.05:1 Ce/Ni.
2. A method according to claim 1 wherein the cerium to nickel atomic ratio is 0.66:1 to 0.1:1.
3. A method according to claim 1 wherein the feedstock is treated with the cerium on a continuous basis.
4. A method according to claim 2 wherein the feedstock is treated with the cerium on a continuous basis.
5. A method according to claim 3 or 4 wherein the cerium is provided through the treatment of the feedstock with cerium octoate.
6. A method according to claim 3 or 4 wherein the cerium is provided through the treatment of the feedstock with cerium nitrate.
7. A method according to claim 3 or 4 wherein the cerium is provided through the treatment of the feedstock with cerium oxide.
8. A method according to claim 7 wherein the cerium oxide is in a water or hydrocarbon based suspension.
Priority Applications (7)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07/208,202 US4913801A (en) | 1988-06-17 | 1988-06-17 | Passivation of FCC catalysts |
| CA000597043A CA1323852C (en) | 1988-06-17 | 1989-04-18 | Passivation of fcc catalysts |
| AU35082/89A AU605425B2 (en) | 1988-06-17 | 1989-05-22 | Passivation of fcc catalysts |
| DE89306138T DE68908791T2 (en) | 1988-06-17 | 1989-06-16 | Hydrocarbon cracking process. |
| EP89306138A EP0347248B1 (en) | 1988-06-17 | 1989-06-16 | Cracking of hydrocarbons |
| AT89306138T ATE93884T1 (en) | 1988-06-17 | 1989-06-16 | HYDROCARBON CRACKING PROCESS. |
| US07/500,426 US5064524A (en) | 1988-06-17 | 1990-03-28 | Passivation of FCC catalysts |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07/208,202 US4913801A (en) | 1988-06-17 | 1988-06-17 | Passivation of FCC catalysts |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US07/500,426 Continuation US5064524A (en) | 1988-06-17 | 1990-03-28 | Passivation of FCC catalysts |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US4913801A true US4913801A (en) | 1990-04-03 |
Family
ID=22773642
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US07/208,202 Expired - Fee Related US4913801A (en) | 1988-06-17 | 1988-06-17 | Passivation of FCC catalysts |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US4913801A (en) |
| EP (1) | EP0347248B1 (en) |
| AT (1) | ATE93884T1 (en) |
| AU (1) | AU605425B2 (en) |
| CA (1) | CA1323852C (en) |
| DE (1) | DE68908791T2 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5064524A (en) * | 1988-06-17 | 1991-11-12 | Betz Laboratories, Inc. | Passivation of FCC catalysts |
| US5378349A (en) * | 1993-05-26 | 1995-01-03 | Phillips Petroleum Company | Passivated catalysts for cracking process |
| US5407560A (en) * | 1992-03-16 | 1995-04-18 | Japan Energy Corporation | Process for manufacturing petroleum cokes and cracked oil from heavy petroleum oil |
| US5853568A (en) * | 1997-07-30 | 1998-12-29 | Exxon Research And Engineering Company | Fluid cat cracking heavy using stripped catalyst for feed preheat and regenerator temperature control |
| US5935890A (en) * | 1996-08-01 | 1999-08-10 | Glcc Technologies, Inc. | Stable dispersions of metal passivation agents and methods for making them |
| US20110132808A1 (en) * | 2011-01-12 | 2011-06-09 | Basf Corporation | Rare Earth-Containing Attrition Resistant Vanadium Trap for Catalytic Cracking Catalyst |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0514597A1 (en) * | 1989-11-08 | 1992-11-25 | Texaco Development Corporation | Reduction of sulfur content in regenerator off gas of a fluid cracking unit |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5064524A (en) * | 1988-06-17 | 1991-11-12 | Betz Laboratories, Inc. | Passivation of FCC catalysts |
| US5407560A (en) * | 1992-03-16 | 1995-04-18 | Japan Energy Corporation | Process for manufacturing petroleum cokes and cracked oil from heavy petroleum oil |
| US5378349A (en) * | 1993-05-26 | 1995-01-03 | Phillips Petroleum Company | Passivated catalysts for cracking process |
| US5935890A (en) * | 1996-08-01 | 1999-08-10 | Glcc Technologies, Inc. | Stable dispersions of metal passivation agents and methods for making them |
| US5853568A (en) * | 1997-07-30 | 1998-12-29 | Exxon Research And Engineering Company | Fluid cat cracking heavy using stripped catalyst for feed preheat and regenerator temperature control |
| US20110132808A1 (en) * | 2011-01-12 | 2011-06-09 | Basf Corporation | Rare Earth-Containing Attrition Resistant Vanadium Trap for Catalytic Cracking Catalyst |
| US9029291B2 (en) | 2011-01-12 | 2015-05-12 | Basf Corporation | Rare earth-containing attrition resistant vanadium trap for catalytic cracking catalyst |
| US9637688B2 (en) | 2011-01-12 | 2017-05-02 | Basf Corporation | Rare earth-containing attrition resistant vanadium trap for catalytic cracking catalyst |
| US10066170B2 (en) | 2011-01-12 | 2018-09-04 | Basf Corporation | Rare earth-containing attrition resistant vanadium trap for catalytic cracking catalyst |
Also Published As
| Publication number | Publication date |
|---|---|
| DE68908791T2 (en) | 1993-12-16 |
| EP0347248B1 (en) | 1993-09-01 |
| DE68908791D1 (en) | 1993-10-07 |
| ATE93884T1 (en) | 1993-09-15 |
| AU605425B2 (en) | 1991-01-10 |
| AU3508289A (en) | 1989-12-21 |
| EP0347248A1 (en) | 1989-12-20 |
| CA1323852C (en) | 1993-11-02 |
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